US2113680A - Method anx apparatus fob defrost- - Google Patents

Method anx apparatus fob defrost- Download PDF

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US2113680A
US2113680A US2113680DA US2113680A US 2113680 A US2113680 A US 2113680A US 2113680D A US2113680D A US 2113680DA US 2113680 A US2113680 A US 2113680A
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/60—Details about pipelines, i.e. network, for feed or product distribution
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/902—Apparatus
    • Y10S62/91—Expander

Description

April 12, 1938. w. L. DE BAUFRE 2,113,680
METHQD AND APPARATUS FOR DEFROSTING AIR SEPARATION PLA NTS Filed Aug. 16, 1935 v 55 them.
Patented Apr. 12, 1938 UNITED STATE,
METHOD AND lirrmarusroa mimosa ING AIR SEPARATION PLANTS- William Lane Baufre, Lincoln, Nebr. Application August "16, 1935, Serial No. 36,551
' 12 Claims? .(Cl. se -175.5) we I I This invention relates to the art of'l iquefying Two air separation plants are shown in. the and separating gases below atmospheric temper drawing. One plant is shown 'in considerable ature in plants where moisture collects as frost" detail in order todescribe the steps in the deduring normal operation and it is necessary to frosting process; 'Ihe other plant isshown only interrupt normal operation at intervals in order in suflicient detallzto describe its relation to the 5 to defrost the various parts of the plants. The first air separation plant during the defrosting invention is particularly applicableto plants for process. In. both plants, we have two interrectifying atmospheric "air into more or. less changers A and B, a liquefler C, an exchanger K, pure oxygen and nitrogen, as atmospheric air al- I a rectifying column H, an expansion engine D, ways contains moisture. A fraction of such moisand a blower S with motor Q and heater T, these 10 ture accumulates as frost in the rectifier, the letters being marked withprimes in the second expansion engine and the heat exchangers of plant.
such plants even when chemical dryingof the The normal operation of these air separation air is resorted to before the air is subjected to plants will not be described in detail because wev the separation process. are here interested in the process of defrosting 15' Heretofore, such plants havebeen defrosted by them rather than in their normal operation. In blowing through them air from the compressor designating the various parts of these plants, the for supplying the compressed air to be processed same letters and figures have been used as in during normal operation. The air for defrosting U. S. Patent No. 1,951,185, issued March 13, 1934.
has followed the same path through the plant as Reference m y be m to s Pat or a de- 20 Y the compressed air during normal operation. scription of the normal operation of the plants Before entering the plant, the air for defrosting shown in the drawing of t Present pp t has been heated and various drainvalves on the As a foundation for some of the claims in this plant have been opened until warmair issued pp however, it y he Said that during therefrom. Since less air was desired for defrost-g n rmal p ti compressed air t s p pe 25 ing than was supplied for processing during n0r-- and flows through the compressed air spaces mal operation, a large portion of the airhandled within interchangers A and B .where it is cooled by th compressor ha usually bee wa t d b by heat transfer to returning products of recticause the compressors have rarely been arranged fi at on. more or less pureoxyge and nitrogen,
to operate continuouslybelow normalspeed or flowing r h the oxy en and nitrogen sp e 30 otherwise with reduced capacities. With a small n p t yone Portion of t e cooled 'air separation plant as u ually employed in makm r s d a s p ed t ugh en in D. ing oxygen for cutting and welding purpose th Another portion of the cooled compressed air waste of power inrunning the compressdf at full nters liquefier- C where it is more or less liquespeed during defrosting is ,not soobjectionable fled y r n r to re urning oxygen and 35 at it would be with large plants for supplying oxynitrogen flowing through the y e and n trogen gen for gas making or for metallurgical furnaces. Spaces therein- The more less liquefied p rt o One object of the present invention is to reduce o co s air is throttled into the lower par waste of power in: defrosting an. air separation of l fi v The expanded P o so en- 4 plant-{ I v v ters the lower part of the rectifier where the pre- 40 Another'object of the invention is to increase m y stage of re i n o c r The final the thoroughness of the defrosting 0perat1on, stage of thetwo-stage rectification occurs in the Another objectof the invention is to decrease l -DP P Of the rectifier from which more or the period of time required to'defrost an air less pure oxygen and nitrogen return through separation plant. v liquefierv C and interchangers A and B. 45
' Another objectof the invention is to enable Dur ne no e t n of the two air epa the rectifier of an air'separation plant-to be thin Plants Shown in the drawing, o e or less operated continuously over long periods of time. pur ni leaves the P s through n r g n The foregoing, togetherwith such other adreturn pipes 61 and 68 respectively and is disvantages as hereinafter appear or are incidentto charged through the common nitrogen main 69 5 the invention, are realized by the construction into whichaother air separation plants not shown illustrated in preferred form in the drawing, may also discharge their waste nitrogen. This which shows a schematic arrangement of air waste nitrogen is almost free of water vapor by separation plants including means for defrosting reason ofv having been cooled to nearly two hundred degrees below zero centigrade in the process of rectifying the air which has been separated into oxygen and nitrogen.
It is proposed to use this moisture free nitrogen for defrosting rather than employ moisture saturated air from the compressors for supplying compressed air to the air separation plants. Even without heating, such moisture free gas would have considerable avidity for absorbing water vapor. But the operation of compressing this nitrogen in order to blow it through a plant will raise its temperature above atmospheric temperature. Further heating may be applied to increase the heat energy available for raising the temperature of cold metal parts ofthe plant above room temperature and for evaporating frost adhering thereto.
It is further proposed to blow this warm dry nitrogen into the air separation plants through their nitrogen outlet pipes in a reverse direction to the flow of nitrogen discharged therefrom during normal operation. This is proposed because ample cross-sectional area for flow of nitrogen from the rectifying column through the liquefier and interchangers is generally provided to give a small pressure drop with a large flow of nitrogen at about atmospheric pressure. Consequently, the warm dry nitrogen will encounter little frictional resistance in flowing into the coldest parts of the air separation plant to defrost it. Also, no special defrosting pipe connections are required, which would increase heat leak into cold parts of the apparatus during normal operation. By means of one special cross-over pipe not required during normal operation, the whole plant may be directly reached by the flow of warm dry nitrogen and thereby thoroughly defrosted.
It is proposed to apply this method of defrosting to two or more air separation units, utilizing in each unit while shut down for defrosting, dry nitrogen discharged from the remaining units in normal operation. But even when the remaining units are not in normal operation or there is a single unit only, the
method of defrosting by blowing atmospheric air into the plant through the nitrogen outlet pipe is superior to the usual method of forcing atmospheric air into the plant through the compressed air inlet pipe.
Referring to the drawing, assume the air separation plant in the lower left hand corner to be in normal operation, discharging moisture free nitrogen through pipe 68 into main 69, valves 64 and 66 being closed and valve 62 open. Assume that the other air separation plant shown in detail, has been shut down and accumulated liquefied gases drained therefrom. Close valve 6! and open valves 63 and 65. Then start blower S and turn on heat in heater T. Dry nitrogen will then be withdrawn from main 69, compressed and heated by compression in blower S, further heated in heater T, and then discharged into the separation plant through pipe 6'! in the reverse direction to the fiow of nitrogen through pipe 61 during normal operation.
Valves l0 and I3 being open, the warm dry nitrogen will flow up through most of the tubes within interchangers A and B. These interchangers will be warmed to the temperature of the warm dry nitrogen and any frost therein melted. Such frost will not be in the nitrogen space within the tubes through which the warm dry nitrogen is flowing, but will be in the com pressed air space outside of these tubes. The
resulting water may be drained out of the compressed air spaces through valves HI and H.
The dry nitrogen will continue its course through pipe 12 and through most of. the tubes within liquefier C. When interchangers A and B have become warmed, the dry nitrogen leaving them will remain warm, and liquefier C will then be warmed. No frost will exist in the nitrogen space within the tubes in liquefier C, but frost will be found in the compressed air space outside these tubes. Such frost will be melted and may be drained out of liquefier C through valve I3.
Continuing its course, the dry nitrogen will flow through pipe 35 (assuming valve 54 closed and valve 83 open) to the top of rectifier H. With valves 3| and 44 closed and drain valves 52 and H open, the dry nitrogen will flow down through the trays indicated in the upper section of rectifier H, through pipes 33, 34 and 4| to the spaces surrounding the tubes in vaporizer G and exchanger K. These parts of the rectifier will be dried and warmed when the dry nitrogen leaving liquefier C becomes warm.
By opening valves 3| and 44, warm dry nitrogen may be discharged from upper section H to lower section F of the rectifier. A more direct path for flow of warm dry nitrogen is provided from liquefier C to lower section F, however, by opening special by-pass valve 54. Assuming the valves in the expansion engine to be closed and drain valves 15 and 16 to be open, this warm dry nitrogen will defrost lower section F of the rectifier and the spaces not previously defrosted within vaporizer G and exchanger H.
To defrost engine D, valve 11 is closed. Inlet and outlet valves 18 and 19 are blocked open. This can readily be done by placing distance pieces and 8| between the valve stems and the tappet rods as shown. The warm dry nitrogen will then flow through the expansion engine from outlet to inlet, thence through pipes l6, l5 and 8, through valves 6 and l, and finally through drain valves 10, H and 13. The defrosting of liquefier C and interchangers A and B will thereby be completed as well as engine D. By opening drain valve 82, the lower part of engine D is warmed and dried.
When the nitrogen blowing from all drain valves feels warm, this indicates that all frost has been melted and drained out as water or vaporized and blown out in the moisture laden nitrogen. Any further vaporization of ice or water at any point within the plant would result in cooling the nitrogen at that point with the result that the nitrogen blowing from a nearby drain valve would not feel warm.
Blower Q is preferably of the centrifugal type which does not require internal lubrication and therefore does not affect the dryness of the nitrogen compressed. A positive displacement type of compressor may, however, be used. Heater T may supply the additional rise in temperature by means of hot water, steam, or electrical energy.
Instead of using a separate blower and heater for each separation unit as shown in the drawing, a single blower and heater may be employed to withdraw dry nitrogen from main 6!! and discharge it through a manifold to any separation unit to be defrosted.
The dry nitrogen from a single unit air separation plant might be stofid and later utilized for defrosting the plants Usually, however, it would be preferable to utilize atmospheric air dry nitrogen, liquefier C and engine D may be heated to or above room temperature and rectif fier H permitted to remain cold without any dan-- ger of depositing moisture therein, particularly'. by passing the dry nitrogen through the nitrogen spaces within the interchangers and the liquefierinstead of storing nitrogen.v Such atmospheric air would need to'be heated after compression because it would be at or near the moisture saturation point due to compression; In flowing through a cold-plant, such atmospheric air would be cooled below the dew point and deposit moisture therein. In parts of theplant, it would be cooled below the freezing point and deposit frost therein. Consequently, in employing atmospheric air for defrosting, conditions with regard to moisture and frost are first made worse within the plant before they are improved. This would not. be true in using dry nitrogen for defrosting. Ac-
.cumulated frost would immediately begin to vaas proposed herein. Frost in rectifier H will be absorbed by the dry nitrogen and carried out of a the rectifier while the rectifier is still below "freezin the rectifier. As soon as liquefier 05a ing temperature. By stopping the defrosting p-j eration before the rectifier has been warmed to room temperature refrigeration is conserved in] and a blower for forcing said warm gas into said 'p lant' through said nitrogen outlet pipe, whereby frost deposited on the heat transferring surfaces in cooling the moist air to be separated is varecooling the rectifier to operating .temperature; By closing valve 83 in pipe 35, valve." infpipey' l8 and valve 29 in pipe 28, interchangers-Amid- B, liquefier C and engine D'may be defrosted iil the manner previously explainedwithout dej liquefied gases may be permitted to remain with gine D have been defrosted, they may. a to operating temperatures and: -the1zplant u into normal operation again withvery little of time. In this way, liquefier C and,eng may be defrosted more frequentlyIthan tifier H. l
By providing means for defrosting for one rectifier and keep the rectifier in continuous operation by alternately defrosting and cooling down the two sets of interchangers, liquefier and expansion engine.
I claim:
1. Method of defrosting air separation plant with interchangers for cooling and liquefier for partly liquefying said air by heat transfer to sep arated oxygen and nitrogen and a rectifier for separating said air into oxygen and nitrogen, including blowing a warm gas through thenitrogen spaces in said interchangers and said liquefier and thence into said rectifier through the nitrogen outlet pipe therefrom and discharging moisture laden gas from said rectifier.
2. Method of defrosting air separation plant; with interchangers for cooling and liquefier for partly liquefying said air by heat transfer to,
separated oxygen and nitrogen and a .two'-s tage rectifier having preliminary and final stages'for separation of said air into oxygen and nitrogen,
frosting rectifier H. In .doing*so,iaccumulated' including blowing a. warm gas through the nitrogen spaces in said interchangers 'andsaid liquefier and thence into the preliminary stage of said rectifier anddischarging moisture laden gas from the preliminary stage'of said rectifier. 3. Method of defrosting air separation plant with interchangers for cooling" and liquefier for partly liquefying said air by heat transfer to separated oxygen and nitrogen and an engine for expanding a portion of said air, including blowing a warm gas through the nitrogen spaces in said interchangers and said, liquefier and thence through said expansion engine.
4. Apparatus for defrosting air separation plant including a nitrogen outlet pipe from said plant,
a valve for closing the ,nitrogen outlet pipe, 2.
' source of nitrogen connected to the nitrogen outlet pipe beyond said valve, a blower for withdrawing gas from the nitrogen outlet pipe beyond said valve, compressing said gas and discharging it into the nitrogen outlet pipe on the other side of said valve whereby said gas is forced into said plant through the nitrogen outlet pipe.
- 5. Apparatus for defrosting air separation plant as in claim 4 including means for heating said gas. I
' 6 In an air separation plant having an interchanger for cooling moist air to be separated by heat exchange through heat transferring surfas to the-separated products and a rectifier for separating the air into said products, apparatus for defrosting said air separation plant including a nitrogen outlet pipe from said interchangenia source of gas external to said air separation plant, means for warming said gas,
pori'z' edand the surfaces dried by heat transfer from'j the'warm gas flowing through the nitrogen spaces within said interchanger.
' 7; Apparatus for defrosting air separation plant including multiple air separation units, a common nitrogen outlet pipe from said units, and means for withdrawing nitrogen from said common nigfi-trogenfoutlet pipe and blowing said nitrogen through one of said units.
l v 8.-A'pparatus for defrosting air separation plant met, "including multiple air separation units with nichangers, liquefier and expansion engine offanz. air separation plant without warming up; -tn -1 e-- tifier, it becomes possible to provide twofsets'of interchangers, liquefier and expansionl' -enginef trogen outlet pipes joined to a common main and means for producing a reversed flow of gas from said common main through one of said nitrogen outlet pipes.
9. Apparatus for defrosting a plant for rectification of gaseous mixtures below room temperature including multiple rectification units and means for blowing through one of said units a product of rectification from another of said surfaces to the separated products, an engine for expanding another part'of the cooled air, and a rectifier for separating the liquefied and expanded air into said products, apparatus for' defrosting said air separation plant including a source of gas external to said air separation plant, means for warming said gas, a blower for forcing said- 2,11s,eso
aration plant including a nitrogen outlet pipe from said interchanger and means for forcing said warm gas into said air separation plant through said nitrogen outlet pipe, whereby frost deposited on the heat transferring surfaces in cooling the moist air to be separated is vaporized and the surfaces dried by heat transfer from the warm gas flowing through the nitrogen spaces within said interchanger.
WILIJAMIANEDEBAUFRE.
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Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2496380A (en) * 1946-04-18 1950-02-07 Elliott Co Gas purifying method and apparatus
US2534478A (en) * 1947-03-31 1950-12-19 Elliott Co Gas purifying method and apparatus
US2553550A (en) * 1946-06-06 1951-05-22 Little Inc A Control for oxygen producing apparatus
US2568223A (en) * 1944-10-20 1951-09-18 Baufre William Lane De Process and apparatus for extracting oxygen from atmospheric air
US2584381A (en) * 1947-05-16 1952-02-05 Barnett F Dodge Low-pressure gaseous o2 cycle with no chemical air purification
US2586026A (en) * 1948-07-21 1952-02-19 Air Liquide Process for the removal of carbon dioxide from gases by cooling
US2716333A (en) * 1946-04-11 1955-08-30 Little Inc A Method and means for treating gases
US2881595A (en) * 1953-10-28 1959-04-14 Air Prod Inc Separation of gaseous mixtures
US2881599A (en) * 1954-01-15 1959-04-14 Philips Corp Device for thawing an ice separator used in a system comprising a cold gas refrigerator
US2934909A (en) * 1954-11-03 1960-05-03 Philips Corp System comprising a refrigerator intended for fractionating gas mixtures
US2975605A (en) * 1955-09-27 1961-03-21 Stamicarbon Process for purifying technical hydrogen
US3174293A (en) * 1960-11-14 1965-03-23 Linde Eismasch Ag System for providing gas separation products at varying rates
US3237418A (en) * 1960-10-26 1966-03-01 Philips Corp Apparatus and method for producing liquid oxygen and/or liquid nitrogen by low temperature rectification of atmospheric air
US3415069A (en) * 1966-10-31 1968-12-10 Nasa High pressure helium purifier
US3418820A (en) * 1966-11-14 1968-12-31 Judson S. Swearingen Method and apparatus for removing vapors from gaseous mixtures by freezing
US3421333A (en) * 1964-08-28 1969-01-14 Linde Ag Thawing technique for a single air separation plant
US3438220A (en) * 1966-11-14 1969-04-15 500 Inc Expansion engine for cryogenic refrigerators and liquefiers and apparatus embodying the same
US20120180520A1 (en) * 2009-09-28 2012-07-19 Koninklijke Philips Electronics N.V. Sytem and method for liquefying and storing a fluid
FR3069916A1 (en) * 2017-08-03 2019-02-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD OF DEFROSTING AN AIR SEPARATION APPARATUS BY CRYOGENIC DISTILLATION AND APPARATUS ADAPTED TO BE DEFORMED THEREBY
EP3438585A3 (en) * 2017-08-03 2019-04-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for defrosting a device for air separation by cryogenic distillation and device adapted to be defrosted using this method

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2568223A (en) * 1944-10-20 1951-09-18 Baufre William Lane De Process and apparatus for extracting oxygen from atmospheric air
US2716333A (en) * 1946-04-11 1955-08-30 Little Inc A Method and means for treating gases
US2496380A (en) * 1946-04-18 1950-02-07 Elliott Co Gas purifying method and apparatus
US2553550A (en) * 1946-06-06 1951-05-22 Little Inc A Control for oxygen producing apparatus
US2534478A (en) * 1947-03-31 1950-12-19 Elliott Co Gas purifying method and apparatus
US2584381A (en) * 1947-05-16 1952-02-05 Barnett F Dodge Low-pressure gaseous o2 cycle with no chemical air purification
US2586026A (en) * 1948-07-21 1952-02-19 Air Liquide Process for the removal of carbon dioxide from gases by cooling
US2881595A (en) * 1953-10-28 1959-04-14 Air Prod Inc Separation of gaseous mixtures
US2881599A (en) * 1954-01-15 1959-04-14 Philips Corp Device for thawing an ice separator used in a system comprising a cold gas refrigerator
US2934909A (en) * 1954-11-03 1960-05-03 Philips Corp System comprising a refrigerator intended for fractionating gas mixtures
US2975605A (en) * 1955-09-27 1961-03-21 Stamicarbon Process for purifying technical hydrogen
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EP3438585A3 (en) * 2017-08-03 2019-04-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for defrosting a device for air separation by cryogenic distillation and device adapted to be defrosted using this method
US10794630B2 (en) 2017-08-03 2020-10-06 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for separating air by cryogenic distillation
US10866024B2 (en) 2017-08-03 2020-12-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation

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